US5053203A - Installation for the fluidized-bed catalytic cracking of a hydrocarbon feedstock - Google Patents

Installation for the fluidized-bed catalytic cracking of a hydrocarbon feedstock Download PDF

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Publication number
US5053203A
US5053203A US07/302,576 US30257689A US5053203A US 5053203 A US5053203 A US 5053203A US 30257689 A US30257689 A US 30257689A US 5053203 A US5053203 A US 5053203A
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reactor
pipe
elbow
downwardly
sloping
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US07/302,576
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Jean-Louis Mauleon
Jean-Bernard Sigaud
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Total Marketing Services SA
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Compagnie de Raffinage et de Distribution Total France SA
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Assigned to COMPAGNIE DE RAFFINAGE ET DE DISTRIBUTION TOTAL FRANCE reassignment COMPAGNIE DE RAFFINAGE ET DE DISTRIBUTION TOTAL FRANCE ASSIGNMENT OF ASSIGNORS INTEREST. Assignors: MAULEON, JEAN-LOUIS, SIGAUD, JEAN-BERNARD
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
    • C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00477—Controlling the temperature by thermal insulation means
    • B01J2208/00495—Controlling the temperature by thermal insulation means using insulating materials or refractories

Definitions

  • the present invention relates to an installation for the fluidized-bed catalytic cracking of a hydrocarbon feedstock. More particularly, it relates to improvements made to the apparatus commonly used for this purpose with a view to improving the conditions of injection of the regenerated catalyst into the cracking column.
  • FCC Fluid Catalytic Cracking
  • the hydrocarbon feedstock is vaporized by being contacted at high temperature with a cracking catalyst that is kept in suspension by the vapors of the feedstock.
  • the catalyst is separated from the products obtained, stripped, reactivated by combustion of the coke formed during the reaction, and then again contacted with the feedstock to be cracked.
  • the desired lowering of the boiling points is the result of controlled catalytic and thermal reactions, and the FCC process is, of course, carried out in such a way that the conversion section is in thermal equilibrium.
  • the intake of hot regenerated catalyst should be such that it will be able to meet the diverse heat requirements of the reaction section, that is, in particular,
  • Such a process is usually carried out in an installation comprising a tubular reactor, known as a riser, which is supplied at its base with regenerated catalyst particles in a controllable quantity.
  • the catalyst is propelled in a dilute homogeneous phase into the tubular reactor by the injection through a diffuser of steam or of a light hydrocarbon.
  • the diffuser is located at the base of the reactor, below the regenerated-catalyst supply line.
  • the feedstock to be cracked is introduced at a higher level of the reactor through an injector or an array of injectors.
  • the reaction column opens at its top into a chamber which may be concentric with it, for example, and in which the gaseous effluents and the catalyst are separated by means of a ballistic separator and the spent catalyst is stripped.
  • the reaction products are freed from all entrained catalyst in a cyclone system, which may be accommodated in the chamber and at the top of which a discharge line for the effluents is provided, while the collected particles of spent catalyst are reinjected at the bottom of the chamber.
  • a stripping gas usually steam, is fed through a line to a diffuser located at the bottom of the chamber.
  • the particles of spent catalyst so stripped are discharged at the bottom of the chamber to a regenerator with one or two combustion chambers.
  • the catalyst particles are maintained in a fluidized bed by means of an oxidizing fluid which assures the combustion of the coke deposited on the catalyst.
  • the hot regenerated catalyst particles are then discharged from the regenerator to the base of the cracking column, where they are reinjected for a new cycle.
  • the circulation of the catalyst between the cracking column and the regenerator is brought about by the differences in pressure and level between these vessels and by the streams of gaseous fluids injected for the operation of the process.
  • U-shaped sections have therefore been proposed as coupling sections between a reactor and a regenerator disposed on the same level.
  • it is difficult to control the circulation of the catalyst and avoid the formation of slopes in the lower portions, and particularly at the bottom of the U-shaped, where the catalyst tends to accumulate, which necessitates the injection of a booster fluid. If the latter is air, it will pose safety problems in the reactor. If it is steam, it will have an adverse effect on the stability of the catalyst, especially if it is at an elevated temperature. And if inert gases are used, they will give rise to problems of control of the unit, particularly on the level of the dry-gas compressor.
  • J circulation sections therefore have also been proposed, with the regenerator at a lower level than the top of the cracking column, and vertical pipes for the discharge from the regenerator of the regenerated catalyst and for its introduction into the reactor vessel, these two pipes being connected to each other through a third pipe having an ascending slope of about 60 degrees which forms the base of the J.
  • This section also requires the injection of a sizable quantity of lifting gas in the ascending portion.
  • the time of contact of this gas with the hot catalyst is relatively long, being over three seconds.
  • it requires that the feedstock be injected into the column at a level that is higher than the upper end of the ascending portion of the circuit. This is detrimental to optimum atomization of the feedstock, which requires as high an injection pressure as possible.
  • the catalyst suspension may become partially defluidized, with gas collecting in the upper portion of the section, which may result in leakage and loss of static pressure.
  • the slide-gate valve controlling the flow rate is located downstream of the expansion joint and operates in an inclined position, which creates problems of wear and flexibility for the valve body.
  • the angular connection further forces the catalyst to undergo a sudden change of direction, which renders its rehomogenization in an upward flow before being mixed with the feedstock very difficult and entails the risk of erosion of the lower portion of the connection.
  • the present invention seeks to overcome these drawbacks by employing a different technology in which the skin (surface) temperatures of the pipes connecting the regenerator to the riser is held close to ambient temperature, that is, to a temperature which preferably does not exceed 150° C., through an inner cladding of these pipes in the form of a layer of an abrasion-resistant heat-insulating refractory material.
  • the invention further seeks to reduce the wall thickness of the pipes connecting the regenerator and the riser and thus to permit their being bent into shapes different from those of the prior art which promote the movement of the regenerated catalyst particles without loss of velocity and without a pressure drop.
  • the invention also seeks to dispense with the use of expansion joints in the pipes connecting the regenerator and the riser by using these cold-wall pipes.
  • a further aim of the invention is to permit locating the valve or valves for the control of the stream of regenerated catalyst particles in a vertical pipe of the circuit used for these particles while keeping that valve as close as possible to the injection zone at the base of the riser.
  • the invention further seeks to permit the use of a transfer pipe for the regenerated catalyst whose diameter is the same as that of the reaction column.
  • a final aim of the invention is to permit the connection of that pipe to the reaction column to have a curved shape favoring rehomogenization of the catalyst and preventing attrition of the particles.
  • the invention has as one element an installation for the fluidized-bed cracking of a hydrocarbon feedstock, said installation comprising an essentially vertical, upflow tubular type of reactor; means for injection into the reactor of the feedstock to be cracked; means for introduction at the base of the reactor of at least one gas capable of maintaining the catalyst particles in a fluidized bed; means in the upper portion of the reactor for the ballistic separation of the spent catalyst particles and the cracked hydrocarbons; means for regeneration of the spent particles by combustion of the coke deposited thereon; means for conducting the spent particles from the reactor to the regeneration means; and means for recycling the regenerated particles from the regeneration means or from an auxiliary buffer chamber to the base of the reactor, said installation being characterized in that the means for recycling the regenerated catalyst particles to the intake of the reactor comprise, from upstream to downstream, a preferably substantially vertical pipe for the discharge of the regenerated particles from the regeneration means, and a substantially straight pipe connected to the vertical pipe and sloping downward therefrom to the base of the reactor to which it is connected, the downward
  • angles made by the axis of the downward-sloping pipe with the axis of the vertical pipe where they connect, and by the axis of the downward-sloping pipe with the axis of the base of the tubular reactor range from 150 to 120 degrees and from 30 to 60 degrees, respectively. In a preferred embodiment, these angles are about 135 degrees and about 45 degrees, respectively.
  • the curved portion or elbow connecting the downwardsloping pipe to the base of the tubular reactor preferably has a diameter substantially equal to that of the base portion to which it is connected, and the injection of a lifting gas is preferably effected tangentially to the lower portion of that elbow and of the elbow connected to the vertical pipe so as to facilitate maintaining the catalyst in a fluidized phase and to impart to it a gradual and uniform acceleration before it is contacted with the feedstock to be cracked in the reaction zone.
  • This configuration makes possible catalyst circulation velocities at the base of the reactor exceeding those of the prior art, where they generally range from 0.6 to 1.2 meters/second. Because of the arrangement in accordance with the invention, this velocity may range from 0.6 to 3 meters/second, and advantageously from 1.2 to 3 meters/second. This velocity range is particularly advantageous for passing to the ascending regime known as "fast fluidization" of the catalyst in the reaction zone, this regime being established for a range of superficial velocities of from 1.0 to 6 meters/second.
  • the pipes in accordance with the invention may, of course, be made of any suitable material; however, in a preferred embodiment of the invention they comprise a metallic wall that is internally clad with a layer of a heat-insulating material of such thickness that the skin temperature of the pipe is close to ambient temperature. It will thus be possible to reduce the wall thickness of the pipes and to bend them without difficulty for curving them to the shapes desired in the elbows. It will also be possible to connect the downward-sloping pipe to the base of the tubular reactor without any sudden change in diameter.
  • the metal or alloy of which these pipes are made may be a simple carbon steel that is less expensive than the special steels and is easy to bend, to shape or to weld.
  • the heat-insulating material with which the pipe is clad may be an abrasion-resistant refractory material. It is preferably applied as a single layer by the cast/vibrated technique and usually is held in place simply through the arch effect without requiring special anchoring means on the pipe.
  • a first advantage of the installation in accordance with the invention is that it makes it possible to dispense with expansion joints in the pipes supplying the reactor with regenerated catalyst.
  • valve which serves for the control of the flow rate of the regenerated catalyst and generally is of the sliding-gate type, can be installed in the vertical position. It is preferably located in the lower portion of the vertical pipe for the discharge of regenerated catalyst from the regenerator or from an auxiliary buffer chamber.
  • the valve will also be of cold-wall construction, that is, made of steel or of another alloy or metal and internally clad with a heat-insulating refractory material, with only the internal components of the valve, such as the sliding gate, then having to be in direct contact with the hot catalyst and being made of stainless steel or fabricated from surface-treated and heatresistant steels.
  • the thermal stresses to which this control valve is subjected thus being greatly reduced, the temperature limits on the regenerated catalyst can be raised, the valves being used continuously at 900° C. instead of about 785° C. as in the prior art.
  • a further advantage of the invention stems from the fact that the internal components of the valve may be made continuous with the diameter of the pipe in which it is installed, by providing refractory transition cones with precisely specified angles to maintain and assure good fluidization of the catalyst.
  • injections of a supplementary lifting gas may be used to accelerate the catalyst particles at the level of the elbow connecting the downward-sloping pipe to the tubular reactor.
  • An air cushion may thus be created at the level of the lower circumference of these elbows by means of minimal quantities of gas, and steam in particular may be used to this end as fluidizing gas without major risk of deactivation of the catalyst even if it is very hot.
  • the air cushion may be produced conventionally by means of a diffuser of the perforated-plate type or with slots below which an air inlet is located.
  • the diffusers may also consist of simple tubes entering and cut flush with the heatinsulating material and judiciously placed, for example, in a staggered arrangement.
  • the density of the catalyst in the pipes 1 and 2 can then be increased to at least 640 kg/m 3 .
  • This arrangement of the invention is of particular interest in the case of a modernization of an old catalytic cracking installation, where the feedstock injection pressure usually is low and difficult to change without complete modification of the feedstock preheating circuit.
  • FIG. 1 is a diagrammatic drawing in a fragmentary vertical section through an installation in accordance with the invention for the fluidized-bed catalytic cracking of hydrocarbon feedstock.
  • FIG. 2 a diagrammatic drawing of apparatus according to U.S. Pat. No. 4,832,325, of the type into which the present invention (with appropriate modification) can be incorporated.
  • the regenerated catalyst particles are discharged from the regenerator, not shown, through a vertical pipe 1 which is connected to a pipe 2 whose descending axis here is inclined about 135 degrees relative to the axis of pipe 1 and which is connected directly to the base of a tubular vertical feedstock elevator or riser 3.
  • the elbows connecting the inclined pipe 2 to pipe 1 and to the base of the riser 3 have an inwardly curved shape without any sharp edges, and pipe 2 is connected to the riser 3 without any discontinuity in diameter.
  • the elbow which has the angle a 2 forms a continuous curved passage into the bottom of the reactor with the downstream upwardly curved portion of the elbow defining the base of the reactor as shown in the drawing and contains the injector 6.
  • Pipe 2 should be as short as possible, but the length of the downwardly sloping transfer pipe is substantially greater than the length of the upwardly curved portion of the elbow with angle a 2 . In the present case the length of the pipe 2 is about four times the diameter of the pipe.
  • the angle a 1 which the axis of the vertical pipe 1 makes with the axis of the downward-sloping pipe 2 is about 135 degrees, while the angle a 2 which the axis of the downward-sloping pipe 2 makes with the axis of the riser is of the order of 45 degrees.
  • the pipes 1 and 2 and the riser 3 are internally clad with a layer 4 of a heat-insulating refractory material which assures that the pipe will have a skin temperature close to ambient temperature and makes it possible to reduce the wall thickness of the pipes and to use only relatively common metals or alloys such as carbon steel.
  • the pipes can thus be readily bent to obtain the inwardly curved connecting shapes characteristic of the invention.
  • a valve 5 for the control of the flow rate of the regenerated catalyst is disposed in the lower portion of the vertical pipe 1.
  • a slide-gate valve whose body is symmetrically supported on the guides can be used without problems of wear or flexibility of the valve body.
  • the valve 5 is internally clad with a heat-insulating refractory material.
  • a line 6 here feeds stream to a diffuser (not shown) disposed at the base of the riser 3, upstream of the injectors for the feedstock to be cracked for propelling the regenerated catalyst in the form of a homogeneous dilute phase into the reactor.
  • Recycled products may further be introduced into the reactor by means of injectors 8, located downstream of the injectors 7, as described, for example, in Applicants' Assigne's French patent application 2,584,732 equivalent to U.S. Pat. No. 4,818,372, issued Apr. 4, 1989 which is also incorporated herein by reference.
  • the feedstock injectors 7 are located at as low a level as possible in the reactor 33, below the level of the slide-gate valve 5, and preferably at a distance from the elbow which connects pipe 2 of from about 1.5 to 5 times, and preferably from 2 to 4 times, the diameter of that pipe.
  • gas injectors 9 are provided for injecting preferably tangentially a booster fluid such as steam at the level of the elbows connecting pipe 2 to the base 3 of the riser and to pipe 1.
  • This booster gas imparts to the catalyst particles a gradual and uniform acceleration, thus contributing to their being maintained in a fluidized state.
  • the injected gas forms an air cushion along the lower circumference of pipe 2 and of the elbows and prevents any local accumulation of particles.
  • the installation in accordance with the invention thus assures a smooth flow of catalyst, consequently eliminating or limiting the risks of catalyst attrition.
  • FIG. 2 is a diagram of a catalytic cracking apparatus equipped with a fluid introduction system and having a single-stage catalyst regeneration chamber.
  • This is an apparatus for cracking by the FCC process disclosed in U.S. Pat. No. 4,832,825.
  • the apparatus essentially comprises a column 3, known as feedstock elevator or riser, which is fed at its base through the line 2, with regenerated catalyst particles in an amount determined by the opening or closing of a valve 20.
  • the temperature and the density of this regenerated catalyst are rendered uniform by injection at the base of the riser, by means of a first diffuser 21, of a first gaseous fluid introduced through the line 22.
  • the catalyst so arrayed and maintained in a homogenous dense phase fluidized bed is then lifted up homogeneously into the riser by a new injection by means of a second diffuser 23, located above the regenerated catalyst intake in the riser, of a second gaseous fluid which may or may not be the same as the first one and which is introduced through the line 24.
  • the feedstock to be cracked is then introduced into the riser by means of an injector 7.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Catalysts (AREA)
US07/302,576 1988-01-26 1989-01-26 Installation for the fluidized-bed catalytic cracking of a hydrocarbon feedstock Expired - Fee Related US5053203A (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR8800849A FR2626284B1 (fr) 1988-01-26 1988-01-26 Appareil pour le craquage catalytique en lit fluidise d'une charge d'hydrocarbures
FR8800849 1988-01-26

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US (1) US5053203A (fr)
EP (1) EP0326478B1 (fr)
JP (1) JP2755647B2 (fr)
AT (1) ATE71403T1 (fr)
DE (1) DE68900652D1 (fr)
FR (1) FR2626284B1 (fr)
ZA (1) ZA89642B (fr)

Cited By (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5205992A (en) * 1990-05-22 1993-04-27 Shell Oil Company Apparatus for introducing catalyst particles into a moving bed of catalyst
US5509216A (en) * 1993-12-24 1996-04-23 Somos Gmbh Apparatus for drying particulate material
US5552119A (en) * 1992-01-09 1996-09-03 Exxon Research And Engineering Company Method and apparatus for contacting solid particles and fluid
US5554341A (en) * 1994-12-12 1996-09-10 Phillips Petroleum Company Feed zone performance for a cat cracker
US6248297B1 (en) 1988-08-26 2001-06-19 Uop Llc FCC reactor arrangement for sequential disengagement and progressive temperature reduction
KR20020049693A (ko) * 2000-12-20 2002-06-26 윤흥조 원료이송라인용 엘보
US20050058516A1 (en) * 2003-08-19 2005-03-17 Damien Gille Device for the transport of granular solid particles with a controlled flow rate
US20080110804A1 (en) * 2006-11-10 2008-05-15 Veltri Fred J Slurry transfer line
US20090020454A1 (en) * 2007-07-17 2009-01-22 Cunningham Brian A Reduced elevation catalyst return line for a fluid catalytic cracking unit
US20100118641A1 (en) * 2007-02-27 2010-05-13 Outotec Oyj Method and apparatus for controlling a stream of solids
US20100158766A1 (en) * 2004-12-23 2010-06-24 Soni Dalip S Processing of Different Feeds in a Fluid Catalytic Cracking Unit
US20130269527A1 (en) * 2012-04-12 2013-10-17 Kellogg Brown & Root Llc Transfer Line for the Primary Cyclone of a Gasifier
CN112361367A (zh) * 2020-12-10 2021-02-12 湖北金炉节能股份有限公司 一种高温流化炉

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2690922B1 (fr) * 1992-05-07 1994-07-22 Inst Francais Du Petrole Procede et dispositif de craquage catalytique dans deux zones reactionnelles successives.

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US2781234A (en) * 1954-05-18 1957-02-12 Exxon Research Engineering Co Automatic control of standpipe and u-bend aeration
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US4331533A (en) * 1980-07-15 1982-05-25 Dean Robert R Method and apparatus for cracking residual oils
EP0129621A1 (fr) * 1983-06-27 1985-01-02 Exxon Research And Engineering Company Appareillage et procédé pour le craquage catalytique fluidisé d'hydrocarbures et régénération du catalyseur
US4601814A (en) * 1983-05-27 1986-07-22 Total Engineering And Research Company Method and apparatus for cracking residual oils
EP0191695A1 (fr) * 1985-02-07 1986-08-20 COMPAGNIE DE RAFFINAGE ET DE DISTRIBUTION TOTAL FRANCE: Société Anonyme dite Procédé et dispositif d'injection de catalyseur dans un procédé de craquage catalytique à l'état fluide, notamment de charges lourdes
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US4728348A (en) * 1986-08-18 1988-03-01 Exxon Research And Engineering Company Low stress cyclone gas collection systems

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US2219011A (en) * 1936-06-20 1940-10-22 Materials Reduction Company In Apparatus for grinding
US2420129A (en) * 1942-10-23 1947-05-06 Universal Oil Prod Co Controlling the flow of fluidized solids and liquids
US2781234A (en) * 1954-05-18 1957-02-12 Exxon Research Engineering Co Automatic control of standpipe and u-bend aeration
US2943994A (en) * 1958-02-14 1960-07-05 Exxon Research Engineering Co Chemicals coking quenching system
US3692667A (en) * 1969-11-12 1972-09-19 Gulf Research Development Co Catalytic cracking plant and method
US3927479A (en) * 1974-11-26 1975-12-23 Fluid Energy Process Equip Drying mill for wet granular particles
US4331533A (en) * 1980-07-15 1982-05-25 Dean Robert R Method and apparatus for cracking residual oils
US4601814A (en) * 1983-05-27 1986-07-22 Total Engineering And Research Company Method and apparatus for cracking residual oils
EP0129621A1 (fr) * 1983-06-27 1985-01-02 Exxon Research And Engineering Company Appareillage et procédé pour le craquage catalytique fluidisé d'hydrocarbures et régénération du catalyseur
US4675099A (en) * 1983-10-14 1987-06-23 Phillips Petroleum Company Flowing catalyst particles in annular stream around a plug in lift pot
EP0191695A1 (fr) * 1985-02-07 1986-08-20 COMPAGNIE DE RAFFINAGE ET DE DISTRIBUTION TOTAL FRANCE: Société Anonyme dite Procédé et dispositif d'injection de catalyseur dans un procédé de craquage catalytique à l'état fluide, notamment de charges lourdes
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Cited By (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6248297B1 (en) 1988-08-26 2001-06-19 Uop Llc FCC reactor arrangement for sequential disengagement and progressive temperature reduction
US5205992A (en) * 1990-05-22 1993-04-27 Shell Oil Company Apparatus for introducing catalyst particles into a moving bed of catalyst
US5552119A (en) * 1992-01-09 1996-09-03 Exxon Research And Engineering Company Method and apparatus for contacting solid particles and fluid
US5509216A (en) * 1993-12-24 1996-04-23 Somos Gmbh Apparatus for drying particulate material
US5554341A (en) * 1994-12-12 1996-09-10 Phillips Petroleum Company Feed zone performance for a cat cracker
KR20020049693A (ko) * 2000-12-20 2002-06-26 윤흥조 원료이송라인용 엘보
US20050058516A1 (en) * 2003-08-19 2005-03-17 Damien Gille Device for the transport of granular solid particles with a controlled flow rate
US7021870B2 (en) * 2003-08-19 2006-04-04 Institute Francais Du Petrole Device for the transport of granular solid particles with a controlled flow rate
US8986617B2 (en) * 2004-12-23 2015-03-24 Lummus Technology Inc. Processing of different feeds in a fluid catalytic cracking unit
US20100158766A1 (en) * 2004-12-23 2010-06-24 Soni Dalip S Processing of Different Feeds in a Fluid Catalytic Cracking Unit
US20080110804A1 (en) * 2006-11-10 2008-05-15 Veltri Fred J Slurry transfer line
US20100118641A1 (en) * 2007-02-27 2010-05-13 Outotec Oyj Method and apparatus for controlling a stream of solids
US8602693B2 (en) * 2007-02-27 2013-12-10 Outotec Oyj Method and apparatus for controlling a stream of solids
WO2009011804A3 (fr) * 2007-07-17 2009-12-10 Exxonmobil Research And Engineering Company Conduit de retour de catalyseur à hauteur réduite pour une unité de craquage catalytique fluide
CN101754801A (zh) * 2007-07-17 2010-06-23 埃克森美孚研究工程公司 用于流化催化裂化装置的降低高程的催化剂回流管路
WO2009011804A2 (fr) * 2007-07-17 2009-01-22 Exxonmobil Research And Engineering Company Conduit de retour de catalyseur à hauteur réduite pour une unité de craquage catalytique fluide
US8202412B2 (en) * 2007-07-17 2012-06-19 Exxonmobil Research And Engineering Company Reduced elevation catalyst return line for a fluid catalytic cracking unit
AU2008276536B2 (en) * 2007-07-17 2014-01-23 Exxonmobil Research And Engineering Company Reduced elevation catalyst return line for a fluid catalytic cracking unit
AU2008276536A8 (en) * 2007-07-17 2014-05-22 Exxonmobil Research And Engineering Company Reduced elevation catalyst return line for a fluid catalytic cracking unit
CN101754801B (zh) * 2007-07-17 2014-06-11 埃克森美孚研究工程公司 用于流化催化裂化装置的降低高程的催化剂回流管路
US20090020454A1 (en) * 2007-07-17 2009-01-22 Cunningham Brian A Reduced elevation catalyst return line for a fluid catalytic cracking unit
US20130269527A1 (en) * 2012-04-12 2013-10-17 Kellogg Brown & Root Llc Transfer Line for the Primary Cyclone of a Gasifier
US8888899B2 (en) * 2012-04-12 2014-11-18 Kellogg Brown & Root Llc Transfer line for the primary cyclone of a gasifier
CN112361367A (zh) * 2020-12-10 2021-02-12 湖北金炉节能股份有限公司 一种高温流化炉

Also Published As

Publication number Publication date
ATE71403T1 (de) 1992-01-15
ZA89642B (en) 1989-10-25
EP0326478B1 (fr) 1992-01-08
EP0326478A1 (fr) 1989-08-02
FR2626284B1 (fr) 1990-06-08
FR2626284A1 (fr) 1989-07-28
DE68900652D1 (de) 1992-02-20
JP2755647B2 (ja) 1998-05-20
JPH01310733A (ja) 1989-12-14

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